CN103992010A - Combined treatment process of stillage and wine-making wastewater - Google Patents
Combined treatment process of stillage and wine-making wastewater Download PDFInfo
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- CN103992010A CN103992010A CN201410232914.0A CN201410232914A CN103992010A CN 103992010 A CN103992010 A CN 103992010A CN 201410232914 A CN201410232914 A CN 201410232914A CN 103992010 A CN103992010 A CN 103992010A
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- stillage
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- 238000000034 method Methods 0.000 title claims abstract description 54
- 239000002351 wastewater Substances 0.000 title claims abstract description 49
- 238000011514 vinification Methods 0.000 title abstract description 5
- 238000003756 stirring Methods 0.000 claims abstract description 39
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000003860 storage Methods 0.000 claims abstract description 22
- 238000001914 filtration Methods 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000003337 fertilizer Substances 0.000 claims abstract description 20
- 239000000706 filtrate Substances 0.000 claims abstract description 18
- 239000011259 mixed solution Substances 0.000 claims abstract description 16
- 238000002791 soaking Methods 0.000 claims abstract description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 48
- 229910021529 ammonia Inorganic materials 0.000 claims description 24
- 239000002893 slag Substances 0.000 claims description 24
- 238000000855 fermentation Methods 0.000 claims description 18
- 230000004151 fermentation Effects 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000011068 loading method Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 abstract description 6
- 239000007787 solid Substances 0.000 abstract description 5
- 230000002829 reductive effect Effects 0.000 abstract description 3
- 235000013339 cereals Nutrition 0.000 description 12
- 238000012545 processing Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 239000002699 waste material Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- IMQLKJBTEOYOSI-GPIVLXJGSA-N Inositol-hexakisphosphate Chemical compound OP(O)(=O)O[C@H]1[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@@H]1OP(O)(O)=O IMQLKJBTEOYOSI-GPIVLXJGSA-N 0.000 description 2
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- IMQLKJBTEOYOSI-UHFFFAOYSA-N Phytic acid Natural products OP(O)(=O)OC1C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C1OP(O)(O)=O IMQLKJBTEOYOSI-UHFFFAOYSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000011174 lab scale experimental method Methods 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
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- 239000004382 Amylase Substances 0.000 description 1
- 102000013142 Amylases Human genes 0.000 description 1
- 108010065511 Amylases Proteins 0.000 description 1
- 108010059892 Cellulase Proteins 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 235000001014 amino acid Nutrition 0.000 description 1
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Landscapes
- Fertilizers (AREA)
Abstract
The invention discloses a combined treatment process of stillage and wine-making wastewater. The combined treatment process comprises the following steps: simultaneously putting the stillage and the wine-making wastewater into a stillage stirring and soaking tank for stirring to obtain a mixed solution; filtering the mixed solution to obtain lixivium and stillage dregs; sending the lixivium in a lixivium storage tank into an anaerobic reactor to perform an anaerobic biological treatment for 1-2 days; allowing the water generated after the lixivium is subjected to the anaerobic biological treatment in the anaerobic reactor to reflow to the stirring tank through a pump; purifying the generated marsh gas and then recycling the marsh gas in a marsh gas cabinet; and filter-pressing the stillage dregs through a plate-and-frame filter press to obtain filter residues and filtrate, wherein the filter residues are used for producing organic fertilizers and the filtrate reflows to the stillage soaking and stirring tank through the pump. The combined treatment process disclosed by the invention can be used for realizing zero emission of the wastewater in a technological treatment process by recycling the wine-making wastewater in which the stillage is soaked in the technological process, and also can be used for effectively treating solid stillage, so that the pollution is reduced and the energy is saved.
Description
Technical field
The invention belongs to solid waste and technical field of waste water processing, be specifically related to a kind of vinasse and brewing wastewater combined treatment process.
Background technology
Chinese liquor distiller grains is the byproduct of wine-making industry.According to statistics, China produces Chinese liquor distiller grains per year and reaches 2,500 ten thousand tons of left and right, and amount is large and concentrated, if processed not in time, will be putrid and deteriorated, and not only severe contamination surrounding environment, also can waste valuable resource.Therefore, the recycling of vinasse has very important significance to the resources conservation of China and environment protection.
China has obtained certain achievement in the research aspect Chinese liquor distiller grains recycling at present, for example, utilize distillers ' grains to produce glycerine, cultivate edible mushrooms, extract aminoacids complex, trace element, phytic acid, phytic acid ca, protein, make vinegar, produce amylase and cellulase, utilize vinasse anaerobically fermenting to reclaim biogas, produce SCP feed, produce feedstuff protein, produce craboraffin, make dyeing reductive agent with lime fermentation, for former wine, produce again, composting material etc., but vinasse complicated component, water content is high, be difficult for storing, also have the fermentation weighting materials such as rice husk that are difficult for utilization, so still be there is to very large difficulty in the utilization of Chinese liquor distiller grains, but also there is sizable room for development simultaneously, therefore need to propose more advanced Technology, process Chinese liquor distiller grains.
Summary of the invention
The object of this invention is to provide a kind of brand-new vinasse and brewing wastewater combined treatment process, distillery waste soaks by internal recycling the dual purpose that solid vinasse reach brewing wastewater zero release and recycling solid vinasse repeatedly.
For achieving the above object, the present invention is by the following technical solutions: first the vinasse that brewery produces and brewing wastewater stir in fermentation vat and stir and soak at vinasse, stir leach liquor in fermentation vat and enter leach liquor storage pool through filtering, regulate pH of leaching solution to 6.8 ~ 7.2, leach liquor NH
3when-N concentration is suitable, can by leach liquor storage pool anaerobic reactor, carry out anaerobic methane production gas, leach liquor NH
3when-N is too high, after Ammonia blowing-out tower is processed, enter anaerobic reactor again and carry out anaerobic methane production gas, processed waste water is back to agitated pool.In agitated pool, remain ammonia nitrogen that poor slag sloughs with Ammonia blowing-out tower after press filtration and mix and produce fertilizer, after press filtration, filtrate is back to agitated pool.Concrete steps are as follows:
(1) vinasse and brewing wastewater enter vinasse simultaneously and stir fermentation vat and stir, and the organism of the part bio-degradable in vinasse is dissolved in waste water by the effect of stirrer, and churning time is 3 ~ 5d, and temperature is 40 ~ 50 ℃;
(2) will after the filtration of step (1) gained mixed solution, enter leach liquor storage pool, filter residue can be used for doing fertilizer after press filtration, and regulates pH of mixed to 6.8 ~ 7.2;
(3) NH in leach liquor storage pool
3-N concentration can increase along with the backflow of waste water, works as NH
3-N concentration during lower than 400mg/L, can promote methane to produce, and NH
3-N concentration can not produce large impact to anaerobic reaction during lower than 800mg/L yet; And work as NH
3-N concentration can play restraining effect to the generation of methane during higher than 800mg/L, now needs to slough part NH through Ammonia blowing-out tower
3-N makes leach liquor keep good biodegradability, and extrusion rate can reach 95%, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment 1 ~ 2d;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, again participate in the whipping process of vinasse, waste water, after the marsh gas purifying producing, enter biogas cabinet and recycle, after the sludge dewatering of generation, dispose;
(5) the unnecessary NH that in step (3), in leach liquor storage pool, mixed solution is sloughed through Ammonia blowing-out tower
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) in vinasse stirring fermentation vat, remain poor slag and after plate-and-frame filter press press filtration, obtain filter residue and filtrate, filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
The COD volumetric loading of described anaerobic reactor is 10 ~ 15kgm
-3d
-1, inlet COD concentration is 10 ~ 12gL
-1, temperature is 28 ~ 35 ℃, pH is 6.5 ~ 7.8.The bottom of described anaerobic reactor is laid with cyclone water distributor, triphase separator upside and cyclone water distributor correspondence position are provided with gas-liquid separator, between gas-liquid separator and triphase separator and gas collector, establish carry tracheae be communicated with cyclone water distributor between establish return line and be communicated with; Inside reactor six roots of sensation upcast and three downtakes are uniformly distributed, thereby reach the effect of eddy flow water distribution, multiple spot backflow.
In described step (1), the mass ratio of vinasse and brewing wastewater is 1:10 ~ 20
The pH of described step (1) gained mixed solution is 4.3 ~ 5.0.
In described step (3), the operating parameters of Ammonia blowing-out tower is: pH=10 ~ 11, and vapour-liquid ratio is 2000 ~ 3000, temperature is 25 ℃ ~ 35 ℃.
Beneficial effect of the present invention: adopt combined treatment process of the present invention, the brewing wastewater that not only soaks vinasse recycles in processing technological flow, can realize the wastewater zero discharge of process treatment process, and can effectively process solid vinasse, can also produce the methane product of economic worth simultaneously, remain poor slag and produce fertilizer, this treatment process has not only significantly reduced the pollution of vinasse and distillery waste, and has saved water resources and the energy.This treatment process also has the features such as capacity of resisting impact load is strong, and system operation cost is low, stable.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Embodiment 1
As shown in Figure 1, a kind of vinasse and brewing wastewater combined treatment process, step is as follows:
(1) vinasse and brewing wastewater enter vinasse simultaneously and stir fermentation vat and stir (as accompanying drawing
process), the organism of the part bio-degradable in vinasse is dissolved in waste water by the effect of stirrer, and churning time is 3 ~ 5d, and temperature is 40 ~ 50 ℃;
(2) in agitated pool, waste water and vinasse leach liquor mixed solution enter leach liquor storage pool after filtration unit, and regulate pH to 6.8 ~ 7.2(as accompanying drawing
process);
(3) the leach liquor NH in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor while being applicable to and carry out anaerobic biological treatment (as accompanying drawing
process), leach liquor NH
3during-N excessive concentration, can slough part NH through Ammonia blowing-out tower
3-N makes leach liquor keep good biodegradability, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment (as accompanying drawing, process), and the treatment time is 1 ~ 2d;
(4) anaerobic reactor water outlet flows to agitated pool by blowback, again participates in the whipping process of vinasse, waste water (as accompanying drawing
process), after the marsh gas purifying of generation, entering biogas cabinet recycles (as accompanying drawing
process), after the sludge dewatering of generation, dispose (as accompanying drawing
process);
(5) mixed solution NH in leach liquor storage pool
3during-N excessive concentration, through Ammonia blowing-out tower, slough unnecessary NH
3-N, the NH sloughing
3-N through absorption unit reclaim the process of producing fertilizer for remaining poor slag (as accompanying drawing,
process);
(6) vinasse stir and in fermentation vat, to remain poor slag and after plate-and-frame filter press press filtration, obtain filter residue and filtrate (as accompanying drawing
,
,
process), filter residue for the production of fertilizer (as accompanying drawing
process), filtrate is flow in vinasse soaking and stirring pond (as accompanying drawing by blowback
process).
Embodiment 2
The raw methanogenic effect of anaerobism of this art treatment, through the lab scale experiment in laboratory, has obtained desirable effect.
The vinasse that laboratory adopts and brewing wastewater, all from Sichuan white wine brewery, are paddy rice liquor fermentation grain slag, and these vinasse are tawny, have strong white wine smell, and water ratio is 62.2%; Brewing wastewater water quality is: pH=4 ~ 5, SS concentration 600 ~ 700mg/L, COD concentration are about 6000 ~ 8000mg/L.
Get 100g vinasse as in 1000mL beaker, add afterwards brewing wastewater 1000mL, 40 ℃ of heating in water bath, are placed in and on agitator, stir 3d.Each water-quality guideline that records agitation leach mixed solution after stirring finishes is as shown in the table
| Project | pH | COD（mg/L） | NH 3-N（mg/L） | SS（mg/L） |
| Numerical value | 4.7 | 14600 | 280 | 2800 |
Leach liquor pH is adjusted between 6.8 ~ 7.2, carries out afterwards anaerobic gas generation experiment, after an about 15d of aerogenesis cycle, COD and SS content are respectively 2560mg/L and 1358mg/L, and clearance is respectively 82.5% and 51.5%; NH
3-N content has increased by 12.7%; Accumulative total one-period gas production rate is 8146mL, and factor of created gase is up to 107.75mL/g, and methane in sewage gas average content is 68.50%.
Embodiment 3
Ammonia-nitrogen desorption effect in this art treatment, through the lab scale experiment in laboratory, has obtained desirable result.
This tests vinasse used with embodiment 1, waste water be vinasse leach liquor through the water outlet of anaerobic treatment each time, concrete water-quality guideline is as shown in the table
| Project | pH | COD（mg/L） | SS（mg/L） |
| Scope | 6.65~6.95 | 2200~2500 | 1300~1700 |
| On average | 6.8 | 2350 | 1500 |
Get 100g vinasse and be placed in 1000mL beaker, add afterwards 1000mL through the water outlet of anaerobic treatment each time, under 40 ℃ of conditions, stir and soak 3d.Repeat this experiment and can obtain following result: initial vinasse leach liquor NH
3-N content is 300mg/L left and right, every through once immersion-anaerobic treatment circulation, the NH in leach liquor
3-N content increases 250mg/L left and right, thus every circulation three times, NH
3-N concentration just reaches 800mg/L, and this concentration can produce slight restraining effect to anaerobically fermenting, every circulation five times, NH
3-N concentration has reached NH more than just can reaching 1600mg/L
3the toxic limit medium dose of-N to anaerobion, so now need the NH in leach liquor
3carry out stripping.
Laboratory is passed through to different pH values, different vapour-liquid ratio, differing temps, to NH in leach liquor
3the experimental study of-N stripping removal effect, draws the following conclusions: work as pH=10, vapour-liquid ratio is 3000, when temperature is 35 ℃, to NH in vinasse leach liquor
3-N has higher removal efficiency, and clearance is 95.1%, NH after stripping
3-N concentration can reach 60mg/L left and right, can meet continuation circulation immersion vinasse used.
Embodiment 4
Enterprise of this art treatment Yi Mou brewery is on probation, and has obtained desirable effect.
These vinasse and waste water are all taken from Chinese liquor distiller grains and the waste water that certain enterprise of brewery produces.For vinasse and waste water, stir the water quality characteristics of leach liquor afterwards, apply treatment process of the present invention, day processing vinasse stir in fermentation vat and leach liquid measure 100m
3, can reach the processing target of each processing unit steady running, economical and efficient.
Distillery waste and vinasse churning time in vinasse soaking and stirring pond is 3 ~ 5d, and temperature is 40 ~ 50 ℃.
Vinasse stir leach liquor in fermentation vat and enter leach liquor storage pool after installing after filtration, and regulate pH of leaching solution to 6.8 ~ 7.2.
Vinasse leach liquor NH in storage pool
3-N concentration can directly enter anaerobic reactor, NH during lower than 800mg/L
3-N concentration enters anaerobic reactor during higher than 800mg/L after Ammonia blowing-out tower is processed again, and the biogas of its generation enters biogas cabinet and recycles after purifying.
Anaerobic reactor water outlet is directly back to agitated pool by pump, again participates in the whipping process of vinasse, waste water.
Mixed solution NH in leach liquor storage pool
3during-N excessive concentration, through Ammonia blowing-out tower, slough unnecessary NH
3-N, the NH sloughing
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit.
Filter residue is for the production of fertilizer after plate-and-frame filter press press filtration in vinasse stirring fermentation vat, to remain poor slag, and filtrate flows to vinasse by blowback and stirs in fermentation vat.
Following table is vinasse leach liquor influent quality scope
| Project | pH | COD（mg/L） | NH 3-N（mg/L） | SS（mg/L） |
| Scope | 4.3~5.0 | 13350~14200 | 260~320 | 2700~3000 |
After technical process of the present invention is processed, COD and SS content are respectively 2300mg/L and 1468mg/L, and clearance is respectively 83.3% and 47.8%; NH
3-N content has increased by 13.8%; Accumulative total one-period aerogenesis, factor of created gase is up to 110.25mL/g, and methane in sewage gas average content is 65.60%.
Embodiment 5
The vinasse of the present embodiment and brewing wastewater combined treatment process, step is as follows:
(1) vinasse and brewing wastewater in mass ratio 1:10 enter vinasse simultaneously and stir fermentation vat and stir, churning time is 3d, temperature is 50 ℃, obtaining pH of mixed is 4.3;
(2) by step (1) gained mixed solution after filtering, obtain leach liquor and poor slag, leach liquor enters leach liquor storage pool, and regulates pH to 6.8;
(3) NH of leach liquor in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor during lower than 800mg/L and carry out anaerobic biological treatment, NH
3-N concentration can be sloughed 95% NH under optimum conditions through Ammonia blowing-out tower during higher than 800mg/L
3-N, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment, and the treatment time is 1d, and the suitable condition in Ammonia blowing-out tower is pH=10, and vapour-liquid ratio is 2000, and temperature is 35 ℃, and the COD volumetric loading of anaerobic reactor is 10kgm
-3d
-1, inlet COD concentration is 10gL
-1, temperature is 28 ℃, pH is 6.5;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, enters biogas cabinet and recycle after the marsh gas purifying of generation;
(5) NH sloughing through Ammonia blowing-out tower in step (3)
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) step (2) is filtered gained grain slag and after plate-and-frame filter press press filtration, is obtained filter residue and filtrate, and filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
Described.
Embodiment 6
The vinasse of the present embodiment and brewing wastewater combined treatment process, step is as follows:
(1) vinasse and brewing wastewater in mass ratio 1:20 enter vinasse simultaneously and stir fermentation vat and stir, churning time is 5d, temperature is 40 ℃, obtaining pH of mixed is 5.0;
(2) by step (1) gained mixed solution after filtering, obtain leach liquor and poor slag, leach liquor enters leach liquor storage pool, and regulates pH to 7.2;
(3) NH of leach liquor in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor during lower than 800mg/L and carry out anaerobic biological treatment, NH
3-N concentration can be sloughed 95% NH under optimum conditions through Ammonia blowing-out tower during higher than 800mg/L
3-N, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment, and the treatment time is 2d, and the suitable condition in Ammonia blowing-out tower is: pH=11, and vapour-liquid ratio is 3000, and temperature is 25 ℃, and the COD volumetric loading of anaerobic reactor is 15kgm
-3d
-1, inlet COD concentration is 12gL
-1, temperature is 35 ℃, pH is 7.8;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, enters biogas cabinet and recycle after the marsh gas purifying of generation;
(5) NH sloughing through Ammonia blowing-out tower in step (3)
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) step (2) is filtered gained grain slag and after plate-and-frame filter press press filtration, is obtained filter residue and filtrate, and filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
Embodiment 7
The vinasse of the present embodiment and brewing wastewater combined treatment process, step is as follows:
(1) vinasse and brewing wastewater in mass ratio 1:15 enter vinasse simultaneously and stir fermentation vat and stir, churning time is 4d, temperature is 45 ℃, obtaining pH of mixed is 4.5;
(2) by step (1) gained mixed solution after filtering, obtain leach liquor and poor slag, leach liquor enters leach liquor storage pool, and regulates pH to 7;
(3) NH of leach liquor in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor during lower than 800mg/L and carry out anaerobic biological treatment, NH
3-N concentration can be sloughed 95% NH under optimum conditions through Ammonia blowing-out tower during higher than 800mg/L
3-N, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment, and the treatment time is 1d, and the suitable condition in Ammonia blowing-out tower is pH=10, and vapour-liquid ratio is 2500, and temperature is 30 ℃, and the COD volumetric loading of anaerobic reactor is 12kgm
-3d
-1, inlet COD concentration is 11gL
-1, temperature is 30 ℃, pH is 7;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, enters biogas cabinet and recycle after the marsh gas purifying of generation;
(5) NH sloughing through Ammonia blowing-out tower in step (3)
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) step (2) is filtered gained grain slag and after plate-and-frame filter press press filtration, is obtained filter residue and filtrate, and filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
Described.
Embodiment 8
The vinasse of the present embodiment and brewing wastewater combined treatment process, step is as follows:
(1) vinasse and brewing wastewater in mass ratio 1:12 enter vinasse simultaneously and stir fermentation vat and stir, churning time is 3.5d, temperature is 46 ℃, obtaining pH of mixed is 5.0;
(2) by step (1) gained mixed solution after filtering, obtain leach liquor and poor slag, leach liquor enters leach liquor storage pool, and regulates pH to 6.9;
(3) NH of leach liquor in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor during lower than 800mg/L and carry out anaerobic biological treatment, NH
3-N concentration can be sloughed 95% NH under optimum conditions through Ammonia blowing-out tower during higher than 800mg/L
3-N, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment, and the treatment time is 1.5d, and the suitable condition in Ammonia blowing-out tower is: pH=10.5, and vapour-liquid ratio is 2750, and temperature is 28 ℃, and the COD volumetric loading of anaerobic reactor is 14kgm
-3d
-1, inlet COD concentration is 12gL
-1, temperature is 32 ℃, pH is 7.5;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, enters biogas cabinet and recycle after the marsh gas purifying of generation;
(5) NH sloughing through Ammonia blowing-out tower in step (3)
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) step (2) is filtered gained grain slag and after plate-and-frame filter press press filtration, is obtained filter residue and filtrate, and filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
Above working process and result show, vinasse and brewing wastewater combined treatment process that the present invention adopts, can give full play to the advantage of each processing unit, when guaranteeing efficient processing rate, wastewater zero discharge in technical process, reduce to greatest extent running cost, aspect processing solid vinasse, there is certain advantage.
It should be pointed out that the above embodiment can make the invention of those skilled in the art's comprehend, but do not limit the present invention in any way creation.Therefore,, although this specification sheets and embodiment have been described in detail to the present invention, it will be appreciated by those skilled in the art that still and can modify or be equal to replacement the invention; And all do not depart from technical scheme and the improvement thereof of the spirit and scope of the invention, it is all encompassed in the protection domain of the invention patent.
Claims (5)
1. vinasse and a brewing wastewater combined treatment process, is characterized in that step is as follows:
(1) vinasse and brewing wastewater enter vinasse simultaneously and stir fermentation vat and stir, and churning time is 3 ~ 5d, and temperature is 40 ~ 50 ℃, obtains mixed solution;
(2) by step (1) gained mixed solution after filtering, obtain leach liquor and poor slag, leach liquor enters leach liquor storage pool, and regulates pH to 6.8 ~ 7.2;
(3) NH of leach liquor in leach liquor storage pool
3-N concentration can directly enter anaerobic reactor during lower than 800mg/L and carry out anaerobic biological treatment, NH
3-N concentration can be sloughed NH under optimum conditions through Ammonia blowing-out tower during higher than 800mg/L
3-N, enters afterwards anaerobic reactor again and carries out anaerobic biological treatment, and the treatment time is 1 ~ 2d;
(4) water outlet that leach liquor carries out after anaerobic biological treatment through anaerobic reactor flows to agitated pool by blowback, enters biogas cabinet and recycle after the marsh gas purifying of generation;
(5) NH sloughing through Ammonia blowing-out tower in step (3)
3-N reclaims the process of producing fertilizer for remaining poor slag through absorption unit;
(6) step (2) is filtered gained grain slag and after plate-and-frame filter press press filtration, is obtained filter residue and filtrate, and filter residue is for the production of fertilizer, and filtrate is flow in vinasse soaking and stirring pond by blowback.
2. vinasse according to claim 1 and brewing wastewater combined treatment process, is characterized in that: the COD volumetric loading of described anaerobic reactor is 10 ~ 15kgm
-3d
-1, inlet COD concentration is 10 ~ 12gL
-1, temperature is 28 ~ 35 ℃, pH is 6.5 ~ 7.8.
3. vinasse according to claim 1 and brewing wastewater combined treatment process, is characterized in that: in described step (1) vinasse and brewing wastewater mass ratio be 1:10 ~ 20.
4. vinasse according to claim 1 and brewing wastewater combined treatment process, is characterized in that: the pH of described step (1) gained mixed solution is 4.3 ~ 5.0.
5. vinasse according to claim 1 and brewing wastewater combined treatment process, is characterized in that: the suitable condition in described step (3) in Ammonia blowing-out tower is: pH=10 ~ 11, and vapour-liquid ratio is 2000 ~ 3000, temperature is 25 ℃ ~ 35 ℃.
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| CN114853163A (en) * | 2022-05-17 | 2022-08-05 | 中节能工程技术研究院有限公司 | Method for cooperatively treating white spirit vinasse with high rice hull content and high-concentration brewing wastewater |
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